Method of creating carbonic acid within an oil matrix

ABSTRACT

A system and method for cracking, hydrogenating and extracting oil from underground deposits is presented. A system includes injecting syngas into a oil deposit to crack and hydrogenate the oil to produce upgraded oil with a reduced density and viscosity. An acid is created to increase the geological matrix within the oil deposit to allow an increase volume of upgraded oil to flow through the geological matrix. For example, condensing the syngas in the oil deposit produces condensed syngas and this can be combined with combining carbon dioxide with the condensed syngas to produce carbonic acid. The upgraded oil with reduced density and viscosity is extracted from the underground deposit to transport the upgraded oil aboveground.

CROSS REFERENCE TO RELATED APPLICATION

This application claims priority from U.S. Provisional Application Ser.No. 61/476,480 filed Apr. 18, 2011; the disclosure of which isincorporated herein by reference.

BACKGROUND OF THE INVENTION

1. Field of Invention

The current invention relates generally to apparatus, systems andmethods for extracting oil. More particularly, the apparatus, systemsand methods relate to extracting oil from underground deposits.Specifically, the apparatus, systems and methods provide for syngasassisted oil recovery, including at least partially cracking andhydrogenating the oil with syngas.

2. Description of Related Art

A variety of processes are used to recover viscous hydrocarbons such asheavy oil and bitumen from underground deposits. Typically, methods areused in heavy oil or bitumen that are greater than 50 meters deep whereit is no longer economic to recover the hydrocarbon by current surfacemining technologies. Depending on the operating conditions of the insituprocess and the geology of the heavy oil or bitumen reservoir, insituprocesses can recover between 25% and 75% of the oil. The primary focusassociated with producing hydrocarbons from such deposits is to reducethe insitu viscosity of the heavy oil or bitumen so that it can flowfrom the reservoir to the production well. The reduction of the insituheavy oil or bitumen is achieved by raising the temperature and/ordilution with solvent, which is the typical practice in existingprocesses.

The Steam Assisted Gravity Drainage (SAGD) is a popular insitu recoverymethod which uses two horizontal wells (a well pair) positioned in thereservoir to recover hydrocarbons. This method is far moreenvironmentally benign than oil sands mining. In this process, the twowells are drilled parallel to each other by using directional drilling.The bottom well is the production well and is typically located justabove the base of the reservoir. The top well is the injection well andis typically located between 15 and 30 feet above the production well.Anywhere between 4 and 20 well pairs are drilled on a particular sectionof land or pad. All the well pairs are drilled parallel to one another,about 300 feet apart, with half of the well pairs oriented in onedirection, and the other half of the well pairs typically oriented 180°in the opposite direction to maximize reservoir coverage. A 15 footmeter separation is often an optimal gap which allows for the maximumreservoir production due to the most effective impact of the injectedsteam. Although the separation between injector and producer wells areplanned for 15 foot, some wells have as high as 30 foot gaps, reducingproduction capability from that particular zone.

The top well injects steam into the reservoir from the surface. In thereservoir, the injected steam flows from the injection well and loosesits latent heat to the cool heavy oil and bitumen and as a result theviscosity of the heated heavy oil and bitumen drops and flows undergravity towards the production well located below the injection well.

Given the quantity of steam required for the SAGD, energy needed for thesteam generation represents a substantial cost for the SAGD. In additionto the cost, other criteria of the steam generation for the SAGD relateto production of carbon dioxide (CO₂) and water input requirements. Forexample, many governments regulate CO₂ emissions. High costs relative toanother option for the steam generation can prevent use of some optionsfor the steam generation regardless of ability to provide desiredcriteria, such as with respect to the production of CO₂. Burning gas oroil to fuel burners that heat steam generating boilers creates CO₂,which is a greenhouse gas that can be captured by various approaches.While further adding to the cost, capturing the CO₂ from flue gases ofthe burners facilitates in limiting or preventing emission of the CO₂into the atmosphere. In contrast to indirect heating with the boilers,prior direct combustion processes inject steam and CO₂ together into theformation even though injection of the CO₂ into the formation may not bedesired or acceptable in all applications.

Regarding the water input requirements, inability to recycle all of thesteam injected results from having to remove impurities such as sodiumchloride from any recovered water prior to the recovered water beingcombined with other make-up water to feed any steam generation. Limitedwater supplies for the make-up water at locations of where SAGD isapplicable can prevent feasibility of the steam generation. Even ifavailable, expense of purchasing water can incur cost for the SAGD.

Typically, the SAGD process is considered thermally efficient if itsSteam to Oil Ratio (SOR) is 3 or lower. The SAGD process requires about1,200 cubic feet of natural gas to heat the water to produce 1 barrel ofbitumen. As of the end of 2010, the National Energy Board (NEB) ofCanada estimates the capital cost of $18-$22 to produce a barrel ofbitumen by the SAGD method. Because of the high ratio of waterrequirement for the SAGD, an alternative process, method or system toreduce water consumption is desirable.

An alternative process that reduces steam usage is an extension of theSAGD process, the Steam and Gas Push (SAGP) where steam and anon-condensable gas are co-injected into the reservoir. Thenon-condensable gas provides an insulating layer and improves thethermal efficiency of the process, resulting in a reduction of steam.

Another extension of the SAGD process uses a solvent, called VaporExtraction (VAPEX). Similar to SAGD, VAPEX consists of two horizontalwells positioned in the reservoir, whereas the top well is the injectionwell and the bottom well is the production well. In VAPEX, a gaseoussolvent such as propane is injected into the reservoir instead of steam.The injected solvent condenses and mixes with the heavy oil or bitumento reduce its viscosity. Under the action of gravity, the mixture ofsolvent and bitumen flow towards the production well and are pumped tothe surface. A major concern with the VAPEX process is how to controlthe significant solvent losses to the reservoir, which has a tremendousimpact on its economics. Therefore, a better way of extracting heavy oiland bitumen from underground deposits is desired.

SUMMARY OF THE INVENTION

The preferred embodiment of the invention includes a system forcracking, upgrading and extracting oil from underground deposits ispresented. The system includes a gasifier, an injection well and aproduction well. The gasifier creates high pressure, high temperaturesyngas. The high pressure, high temperature syngas flows through theinjection well into a deposit of oil under the ground to crack andhydrogenate the oil to produce upgraded oil with a reduced density andviscosity. The production well of the system receives the reduceddensity and viscosity oil and transports it above the ground where itmay be further separated into a portion that may be sold and a portionthat can be gasified in the gasifier. The system can be configured as asyngas assisted gravity drainage (SYAGD) system of oil recovery. In anSYAGD system, the injection well outputs the syngas above an input ofthe production well so that the reduced viscosity oil can flow downwardinto an input of the production well.

In another configuration of the preferred embodiment, the gasifierincludes an oxygen input, an oil input and a steam input. Oxygen isinput to the gasifier through the oxygen input, oil is input to thegasifier through the oil input and steam is input into the gasifierthrough the steam input. The gasifier mixes the oxygen, oil and gas toproduct the syngas.

In one configuration of the preferred embodiment, the gasifier creates asyngas comprised of hydrogen and carbon monoxide. The ratio of hydrogento carbon monoxide is about 2 to 1. In another configuration of thepreferred embodiment, the ratio of hydrogen to carbon monoxide is about3 to 1.

Another configuration of the system for cracking, hydrogenating andextracting oil from underground deposits includes an oxygen compressorand an emulsification vessel. The oxygen compressor creates a stream ofhigh pressure gasification oxygen and a stream of high pressureatomizing oxygen. The emulsification vessel mixes a stream of oil withthe stream of high pressure atomizing oxygen to produce mixed oil. Themixed oil, high pressure gasification oxygen and steam are input to thegasifier.

Another configuration of the system includes a heat recovery unit (HRU).The HRU reduces and controls the temperature of the syngas before it isinjected to the deposit of oil. The system can also include a closedloop system to recover the heat given up by the syngas at the HRU asrecovered heat to convert the recovered heat into electricity. Theclosed loop system can be an organic rankine cycle (ORC) system.

The closed loop system can include a generator, a heat exchanger, anexpander turbine and an air heat exchanger. The heat exchanger heats andvaporizes a liquid to create a vaporized liquid. The expander turbinereceives the vaporized liquid and generates shaft power to rotate thegenerator. The generator produces electricity. The air heat exchangercools the vaporized liquid back into a liquid by exchanging heat withair. The liquid can be a refrigerant.

Another configuration of the preferred embodiment includes a system witha gasification unit, a compressed oxygen line, an oil line, a steamline, an injection well and a production well. The compressed oxygenline carries compressed oxygen into the gasification unit, the oil linecarries oil into the gasification unit and the steam line carries steaminto the gasification unit. The gasification unit gasifies thecompressed oxygen, oil and steam to produce a syngas stream. Theinjection well carries the syngas stream to an underground deposit ofoil where the syngas cracks and hydrogenates oil in the deposit toproduce upgraded oil and the production well recovers the upgraded oiland transports the upgraded oil above ground. This system can include aheat recovery unit to reduce and control the temperature of the syngasstream before it is sent to the injection well

BRIEF DESCRIPTION OF SEVERAL VIEWS OF THE DRAWINGS

One or more preferred embodiments that illustrate the best mode(s) areset forth in the drawings and in the following description. The appendedclaims particularly and distinctly point out and set forth theinvention. The accompanying drawings, which are incorporated in andconstitute a part of the specification, illustrate various examplemethods, and other example embodiments of various aspects of theinvention. It will be appreciated that the illustrated elementboundaries (e.g., boxes, groups of boxes, or other shapes) in thefigures represent one example of the boundaries. One of ordinary skillin the art will appreciate that in some examples one element may bedesigned as multiple elements or that multiple elements may be designedas one element. In some examples, an element shown as an internalcomponent of another element may be implemented as an external componentand vice versa. Furthermore, elements may not be drawn to scale.

FIG. 1 illustrates a preferred embodiment of a system for upgrading andextracting heavy oil from underground.

FIG. 2 illustrates in more detail the preferred embodiment of the systemfor upgrading and extracting heavy oil from underground.

FIGS. 3A and 3B illustrate how to use the system for upgrading andextracting heavy oil from underground increase the geological matrix toallow oil to more easily flow through the matrix.

FIG. 4 illustrates a configuration of the preferred embodimentrepresented as a method for upgrading and extracting heavy oil fromunderground.

Similar numbers refer to similar parts throughout the drawings.

DETAILED DESCRIPTION

FIG. 1 illustrates a first configuration of the preferred embodiment ofa system 100 for upgrading bitumen, heavy oil or another oil andextracting them from a reservoir 110. FIG. 1 illustrates a configurationof the preferred embodiment of the system that generates a syngas with arather high temperature and pressure that is injected into an injectionwell. While it may not be practical to inject syngas with such hightemperatures and pressures, this Figure is useful for understanding someof the novelty of the invention. After FIG. 1 is discussed, otherfigures that implement more detailed and more practical systems andmethods such as those which reduce the temperature of the syngas beforeit is injected into a well are discussed further.

In FIG. 1, fuel is input to a high pressure gasifier 102 through a feedline 101 along with oxygen from line 120 and steam from line 121. Thefuel is partially burned in the gasifier with the oxygen and steam togenerate a high temperature, high pressure syngas. The high temperatureand high pressure syngas includes primarily hydrogen and carbonmonoxide. In this configuration of preferred embodiment, the ratio ofhydrogen to carbon monoxide in the syngas is in the range of 2 to 3:1.The high pressure gasifier 102 that generates the syngas can be a marketavailable high pressure gasifier such as the ZEEP (Zero Emissions EnergyPlant) gasifier developed by Pratt and Whitney Rocketdyne. U.S. Pat. No.7,547,423 describes other aspects of a high pressure gasifier thecontents of which are incorporated herein by reference. The system 100injects the syngas at a controlled temperature into the reservoir 110 toheat, crack, hydrogenate and upgrade heavy oil insitu. Cracking theheavy oil in the presence of hydrogen can prevent or reduce theformation of coke.

The syngas is transported through an upper well line 104 that transportsit below the Earth's surface 106 to an upper region of an oil reservoir110. The upper well line 104 may be connected to an upper wellhorizontal line 108 that can have openings periodically placed in thehorizontal line 108 to distribute the syngas at periodic intervalswithin the reservoir 110. The heated hydrogen and carbon monoxide of thesyngas entering the reservoir 110 heats up, cracks and hydrogenatesheavy oil within the reservoir providing a higher recovery rate than atypical SAGD system. The cracked and hydrogenated heavy oil has a lowerdensity and viscosity that allows it to flow generally downward toward alower well horizontal line 114. The lower well horizontal line 114 canhave holes periodically placed in it to allow the cracked oil to flowinto these holes. The cracked oil can then be extracted through avertical well line 112 and brought to the surface of the earth forfurther processing and/or storage.

The system 100 for upgrading and extracting heavy oil of FIG. 1 hasseveral benefits over a traditional SAGD system. The system 100 usesvery little water consumption, the consumed steam is the raw materialfor the generation of hydrogen through water gas shift reaction. Unlikea typical SAGD, system 100 for upgrading and extracting heavy oilcreates little to no emissions, because the products of gasification areinjected into the well. The formation of hydrogen in the syngas aids inthe hydrogenation of the cracked heavy oil, upgrading it and minimizingthe formation of coke. Because hydrogen has a heat capacity of 14.3J/g.K versus 2.08 for steam, it provides for superior heat transfer tothe oil reservoir 110. Additionally, the system 100 can have no externalfuel requirements or associated infra-structure because it can use aslipstream of the produced oil bottoms fraction as fuel which results inlower capital and operating costs per barrel of bitumen produced. Usinga slipstream to eliminate or significantly reduce external fuelrequirements is discussed in detail below with reference to the system200 of FIG. 2.

FIG. 2 illustrates a second configuration of the preferred embodiment ofa system 200 for upgrading bitumen, heavy oil or another oil andextracting them from a reservoir 110. Similar to the system 100 of FIG.1, the system 200 of FIG. 2 includes a high pressure gasifier 102 togenerate a high temperature, high pressure syngas of primarily hydrogenand carbon monoxide. Unlike the system of FIG. 1, the system 200 of FIG.2 includes an ORC system 250 with a hot oil circulating loop to allowfor the temperature of the syngas to be lowered and to provide thermalenergy to an ORC power generation unit 208. The components of the ORCsystem 250 and the details of how it operates are discussed below.Lowering the temperature of the syngas allows it to be injected attemperatures between 300° C. and 500° C. into the reservoir reducing theneed to have extremely high performance piping and equipment that wouldbe required at higher pressures and temperatures. Similar to the systemof FIG. 1, the conditioned high pressure hydrogen and carbon monoxidesyngas is routed to the injection well through lines 104 and 114 to heatthe formation, crack the heavy oil in the formation and react with thehydrogen in the presence of a natural catalytic environment of fineclays and sand to upgrade bitumen and/or heavy oil in the productionwell. Again, the high pressure gasifier 102 may be a Pratt and WhitneyRocketdyne ZEEP gasifier or another type of gasifier as understood bythose of ordinary skill in the art.

Before describing further details of the system 200 for upgradingbitumen, heavy oil or another oil, some of the improvements of thissystem are discussed over prior systems. Whereas a typical SAGD systemis limited to heating the oil formation to reduce the oil viscosity, thesystem of FIG. 2 provides the capability for the heating, cracking,hydrogenating and upgrading of heavy oil. Moreover, the system 200 ofFIG. 2 can meet on demand temperatures required in the oil formationwhereas the SAGD process temperature is limited to the rating of thesteam generator pressure which sets the temperature of the injectioninto the reservoir. The system 200 for upgrading bitumen, heavy oil oranother oil, can generate a wide range of injection temperatures ondemand. This ability to control injection temperature allows for bettercontrol of production and larger gaps between injector and producingwells. As a result, it can reduce capital costs substantially. Little tono external power is required to power the system 200 because the system200 generates its own power by recovery of thermal energy in controllingthe temperature of the syngas to reservoir 110.

The system 200 for upgrading bitumen, heavy oil or another oil of FIG. 2includes an air blower 222, a molecular sieve 223 and an oxygencompressor 224 to generate a high concentration oxygen stream to providethe oxygen requirements for the incomplete combustion of the fuel in thegasifier 102. The air blower 222 is provided to first pressurizeatmospheric air. A line carries the compressed air to the molecularsieve 223 where it is separated into O₂ and nitrogen. The nitrogen isreleased into the atmosphere or it can be recovered if desired. Theoxygen compressor 224 further compresses the highly concentrated oxygen.The compressed oxygen leaves the compressor 224 on line 228 which splitsinto a gasification oxygen line 120 and an atomizing oxygen line 125.

The system 200 for upgrading bitumen, heavy oil or another oil includesa feed tank 202 for storing oil reclaimed from the reservoir 110. Aportion of this stored oil from the feed tank 202 is carried from theinput line 101 to a high pressure oil pump 204 that pumps it into line206. Compressed atomizing O₂ from line 225 and the feed oil in line 206are combined and passed through line 226 to an emulsifier vessel 227where they are mixed together.

Steam in line 121, gasification oxygen in line 120 and the emulsifiedoxygen and oil in line 228 all enter the high pressure gasifier 102where they are combined to generate a high pressure, high temperaturesyngas. As previously mentioned when discussing FIG. 1, the gasificationgenerates about a 2 to 3:1 ratio of hydrogen and carbon monoxide. Thoseof ordinary skill in the art will realize that this ratio is selectableand can be other ranges or values. Before the high pressure, hightemperature syngas is injected down line 104 to the reservoir, line 230first carries it to a gasifier heat recovery unit (HRU) 132 to control(e.g., lower) the syngas temperature.

Power is generated in an organic rankine cycle (ORC) system 250 whichconverts the thermal energy captured in the gasifier HRU 132 intoelectricity. The ORC system 250 includes an ORC heat exchanger 234, line240, a generator 208, line 241, an air heat exchanger 242, line 243, arefrigerant pump 244 and line 245. The ORC system 250 receives itsenergy from a closed loop hot oil circulation system including thegasifier HRU 232, line 233, the ORC heat exchanger 234, line 235, pump236, line 237 and the gasifier HRU 232.

The oil circulating system 250 controls the temperature of the syngasfor injection into the reservoir 110. The temperature of the syngas iscontrolled by feeding hot circulating oil in line 233 into the ORC heatexchanger 234 where it gives up its thermal energy. Line 233 transfersheat from the HRU 232 to the ORC heat exchanger resulting in a coolingof the syngas exiting the HRU on line 104. The cooled circulating oiltravels in line 235 to an oil pump 236. Then pump 236 pumps the oilthrough line 237 to a heating coil in the gasifier HRU 237 to completethis loop.

In another closed loop, a low boiling point fluid (a refrigerant) ispumped by refrigerant pump 244 at a high pressure in line 245 to the ORCheat exchanger 234 where it is vaporized to form a high pressure, lowboiling point gaseous fluid. This high pressure, low boiling point fluidgaseous stream enters, from line 240, an expander turbine so that it canprovide shaft horsepower to the generator 208 to provide rotation to anelectrical generator. The rotating electrical generator can then produceelectricity to power the overall system 200 for upgrading bitumen, heavyoil or another oil. Line 241 carries the lower energy stream after itpassed through the generator 208 to the air heat exchanger 242. At theair heat exchanger 242, the lower energy stream is further cooled. Line243 carries the stream from the air heat exchanger 242 back to the pump244 where the cycle begins to repeat in another cycle.

The system 200 for upgrading heavy oil pumps the conditioned heavy oilfrom the HRU 232 in line 104 down to the oil reservoir 110. The syngasis generally injected into line 104 for travel to the reservoir 110 atabout 300° C. to 500° C. Similar to the discussion above with referenceto system 100, the injected syngas heats up the oil formation, cracking,hydrogenating and upgrading the heavy oil, decreasing its density andviscosity allowing it to flow into the production well (e.g., lines 112and 114). The system 200 utilizes the natural catalytic bed of theformation to aid the rate of reaction. For example, the reservoirminerals are composed of clay minerals and non-clay minerals, the clayminerals, such as kaolinites and montmorillonite, are the main catalystsin the process of hydrocarbon source rock organic compounds. Moreoverthe elements of aluminium, iron and potassium present in the matricesare known to promote catalysis oxidation, decarboxylation andhydrogenation of organic compounds.

The high pressure, high temperature gasifier 102 can be controlled sothat the generated syngas includes carbon dioxide. When the syngas steamcondenses in the reservoir 110 it combines with the carbon dioxide toform carbonic acid. Referring to FIGS. 3A/B, the carbonic acid dissolvesthe cement bridges 352 between quartz particles and thus increases thepore space at the geological matrix in the reservoir which will allowthe passage (increases the release) of more oil toward the output welllines 112 and 114 increasing the production of the reservoir. FIG. 3Aillustrates a blown up example of a geological matrix before thecreation of carbonic acid and FIG. 3B illustrates what the samegeological matrix may look like after it has interacted with carbonicacid. Dissolution of CO₂ in the formation water results in the formationof carbonic acid, which in turn dissolve the formation minerals duringinjection, this process improves formation permeability.

Additional carbon dioxide can be injected into the reservoir to furtheract as a pressurizing agent and when dissolved underground in the heavyoil, it significantly reduces its viscosity, enabling the oil to flowmore easily through the wider pore formation into the production well.The system may leave this carbon dioxide underground in the depositafter the oil has been extracted.

The amount of hydrogen that is injected into the reservoir 110 by lines104 and 108 affect the cracking hydrogenation reactions process and thequality of the oil extracted from the reservoir 110. Therefore, thesystem 200 for upgrading bitumen, heavy oil or another oil can includean API gravity meter 300 for monitoring the quality of upgraded oilbeing extracted from the reservoir 110. The API gravity can be monitoredand when it falls out of range of values that system 100 is monitoring,a controller 302 can be configured to adjust the amount of oxygen, steamand/or oil input to the high pressure gasifier 102 to control; theamount and composition of hydrogen in syngas stream; the pressure andtemperature of the syngas being injected into the reservoir 110 to movethe API gravity to a more acceptable range.

Lines 112 and 114 carry the upgraded oil that is recovered in theproduction well and carry it aboveground to a separator 260. Theseparator 260 splits the produced upgraded oil into two streams. Line261 carries a portion of the heavy ends for gasification and line 262carries the light ends for sales.

Example methods may be better appreciated with reference to flowdiagrams. While for purposes of simplicity of explanation, theillustrated methodologies are shown and described as a series of blocks,it is to be appreciated that the methodologies are not limited by theorder of the blocks, as some blocks can occur in different orders and/orconcurrently with other blocks from that shown and described. Moreover,less than all the illustrated blocks may be required to implement anexample methodology. Blocks may be combined or separated into multiplecomponents. Furthermore, additional and/or alternative methodologies canemploy additional, not illustrated blocks.

FIG. 4 illustrates a configuration of the preferred embodiment as amethod 400 for cracking and extracting oil beneath the ground. Themethod 400 is especially well suited to extract oil from depositsbeneath the earth's surface. The method 400 begins by creating a highpressure, high temperature syngas, at 402. As previously mentioned, thesyngas can be created by partial combustion of a mixture of oil, oxygenand steam in a gasifier. Next, the syngas is injected into a deposit ofoil under the ground, at 404, to crack and hydrogenate the oil toproduce upgraded oil with a reduced viscosity. Some configurations ofthe method 400 will cool the syngas in a heat recovery unit before it ispumped below ground. The reduced viscosity oil is extracted and broughtabove the ground, at 406. This oil can be separated into light oil thatis ready for sales and heavier oil that can be used to create the syngasin a gasifier.

In the foregoing description, certain terms have been used for brevity,clearness, and understanding. No unnecessary limitations are to beimplied therefrom beyond the requirement of the prior art because suchterms are used for descriptive purposes and are intended to be broadlyconstrued. Therefore, the invention is not limited to the specificdetails, the representative embodiments, and illustrative examples shownand described. Thus, this application is intended to embracealterations, modifications, and variations that fall within the scope ofthe appended claims.

Moreover, the description and illustration of the invention is anexample and the invention is not limited to the exact details shown ordescribed. References to “the preferred embodiment”, “an embodiment”,“one example”, “an example”, and so on, indicate that the embodiment(s)or example(s) so described may include a particular feature, structure,characteristic, property, element, or limitation, but that not everyembodiment or example necessarily includes that particular feature,structure, characteristic, property, element or limitation. Furthermore,repeated use of the phrase “in the preferred embodiment” does notnecessarily refer to the same embodiment, though it may.

1. A method for extracting oil from an underground oil depositcomprising: injecting syngas into a oil deposit to crack and hydrogenatethe oil to produce upgraded oil with a reduced density and viscosity;creating an acid to increase the geological matrix within the oildeposit to allow an increase volume of upgraded oil to flow through thegeological matrix; and extracting the upgraded oil with reduced densityand viscosity from the underground deposit to transport the upgraded oilaboveground.
 2. The method of claim 1 wherein the creating an acidfurther comprises: creating carbonic acid.
 3. The method of claim 2wherein the creating carbonic acid further comprises: condensing thesyngas in the oil deposit to produce condensed syngas; and combiningcarbon dioxide with the condensed syngas to create carbonic acid.
 4. Themethod of claim 1 wherein the acid dissolves cement bridges betweenquartz particles to increase poor space of the geological matrix.
 5. Themethod of claim 1 further comprising: generating high pressure, hightemperature syngas.
 6. The method of claim 4 further comprising:generating the syngas by incompletely combusting oil with oxygen andsteam.
 7. The method of claim 1 further comprising: reducing thetemperature of the syngas before the syngas is injected to the oildeposit.
 8. The method of claim 1 further comprising: flowing thereduced density and viscosity oil to a production well beneath theearth's surface; and pumping the reduced density and viscosity oil fromthe production well as part of a syngas assisted gravity drainage(SYAGD) method of oil recovery.
 9. The method of claim 8 furthercomprising: pumping the syngas to an injection well that outputs thesyngas above an input of the production well so that the reduced densityand viscosity oil can be assisted by gravity to flow downward into aninput of the production well.
 10. The method of claim 1 wherein thesyngas is comprised primarily of hydrogen and carbon monoxide, whereinthe ratio of hydrogen to carbon monoxide is about 2 to
 1. 11. The methodof claim 1 wherein the syngas is comprised primarily of hydrogen andcarbon monoxide, wherein the ratio of hydrogen to carbon monoxide isabout 3 to
 1. 12. A method of recovering oil from a heavy oil depositcomprising: injecting syngas through an injection well to crack,hydrogenate and reduce the viscosity the heavy oil to produce upgradedoil; generating an acid to increase a geological matrix of the oildeposit for allowing more of the upgraded oil to flow; and recoveringthe upgraded oil and bringing the upgraded oil aboveground through aproduction well.
 13. The method of claim 12 wherein the creating an acidfurther comprises: creating carbonic acid.
 14. The method of claim 13wherein the creating carbonic acid further comprises: condensing thesyngas in the oil deposit to produce condensed syngas; and combiningcarbon dioxide with the condensed syngas.
 15. The method of claim 12further comprising: controlling the temperature of the syngas before thesyngas is sent below the surface of the earth.
 16. The method of claim12 further comprising: cooling the syngas before the syngas is sent tothe injection well.
 17. The method of claim 16 further comprising:generating power with heat removed from the syngas.
 18. The method ofclaim 12 further comprising: separating the upgraded oil into oil forsale and oil for gasification.
 19. The method of claim 13 furthercomprising: generating the syngas by at least partially combusting theoil for gasification.
 20. The method of claim 12 wherein the syngas iscomprised primarily of hydrogen and carbon monoxide where the ratio ofhydrogen to carbon monoxide is about 2.5 to 1.